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New 3-dimensional CFD modeling of CO2 and H2S simultaneous stripping from water within PVDF hollow fiber membrane contactor

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Abstract

In this paper a 3-dimensional modeling of simultaneous stripping of carbon dioxide (CO2) and hydrogen sulfide (H2S) from water using hollow fiber membrane made of polyvinylidene fluoride is developed. The water, containing CO2 and H2S enters to the membrane as feed. At the same time, pure nitrogen flow in the shell side of a shell and tube hollow fiber as the solvent. In the previous methods of modeling hollow fiber membranes just one of the membranes was modeled and the results expand to whole shell and tube system. In this research the whole hollow fiber shell and tube module is modeled to reduce the errors. Simulation results showed that increasing the velocity of solvent flow and decreasing the velocity of the feed are leads to increase in the system yield. However the effect of the feed velocity on the process is likely more than the influence of changing the velocity of the gaseous solvent. In addition H2S stripping has higher yield in comparison with CO2 stripping. This model is compared to the previous modeling methods and shows that the new model is more accurate. Finally, the effect of feed temperature is studied using response surface method and the operating conditions of feed temperature, feed velocity, and solvent velocity is optimized according to synergistic effects. Simulation results show that, in the optimum operating conditions the removal percentage of H2S and CO2 are 27 and 21 % respectively.

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Abbreviations

I:

I-component (CO2 and H2S)

C0 :

Inlet mixture concentration (mol/m3)

C:

Concentration (mol/m3)

Ci-membrane :

Component i concentration in the membrane (mol/m3)

Ci-shell :

Component i concentration in the shell (mol/m3)

Ci-tube :

Component i concentration in the tube (mol/m3)

D:

Diffusion coefficient (m2/s)

Di-membrane :

Diffusion coefficient of component i in the membrane (m2/s)

Di-shell :

Diffusion coefficient of component i in the shell (m2/s)

Di-tube :

Diffusion coefficient of component i in the tube (m2/s)

F:

Body force (N)

Ji :

Diffusive flux of species i (mol/s)

m:

Physical solubility (dimensionless)

r:

Radial coordinate (m)

r1 :

Inner tube radius (m)

r-2 :

Outer tube radius (m)

r-3 :

Inner shell radius (m)

Ri :

Reaction rate of species i (mol/s)

t:

Time (s)

u:

Average velocity in the tube side (m/s)

V:

Velocity vector (m/s)

Vz :

z Direction velocity in the contactor (m/s)

Vz-shell :

z Direction velocity in the shell (m/s)

∇:

Gradient (dimensionless)

ρ:

Density (kg/m3)

η:

Dynamic viscosity (m2/s)

in:

Inlet

out:

Outlet

Vz-tube :

z Direction velocity in the tube (m/s)

Vinlet :

Inlet velocity to the contactor (m/s)

z:

Axial distance (m)

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Author information

Authors and Affiliations

  1. Department of Petrochemical Engineering, Amirkabir University of Technology (Tehran Ploytechnic), Mahshahr Campus, Mahshahr, Iran

    Ahmad Bahlake

  2. Department of Chemical Engineering, Amirkabir University of Technology (Tehran Ploytechnic), Tehran, Iran

    Foad Farivar & Bahram Dabir

  3. Energy Research Center, Amirkabir University of Technology (Tehran Ploytechnic), Tehran, Iran

    Bahram Dabir

Authors
  1. Ahmad Bahlake
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  2. Foad Farivar
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  3. Bahram Dabir
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Corresponding author

Correspondence to Bahram Dabir.

Appendix

Appendix

1.1 Solubility

The distribution coefficient of CO2 in pure water is taken from Versteeg and van Swaaij [29]. Also the distribution coefficient of CO2 in pure water was taken from Dindore et al. [30].

$$m_{{water - CO_{2} }} = 3.59 \times 10^{ - 7} RT\exp \left( {\frac{2044}{T}} \right)\;dimensionless$$
(20)
$$m_{{water - H_{2} S}} = 1000 RT \times 10^{ - a} \;dimensionless$$
(21)

where

$$a = 2.7896 + 0.03145T - 4.8104 \times 10^{ - 5} T^{2} \left( {\frac{672.791}{T}} \right) + 0.14423\log T$$
(22)

1.2 Diffusivity

The diffusivity of CO2 in pure water was taken from Versteeg and van Swaaij [29]. The diffusivity of H2S in pure water was taken from Cussler and Edvard [31].

$$D_{{CO_{2} \hbox{-}water}} = 2.35 \times 10^{ - 6} \exp \left( {\frac{ - 2119}{T}} \right)\;{\text{m}}^{2} /{\text{s}}$$
(23)
$$D_{{H_{2} S\hbox{-}water}} = 1.7 \times 10^{ - 9} \;{\text{m}}^{2} /{\text{s}}$$
(24)

The diffusivity of CO2 in N2 can be calculated based on Chapman–Enskog theory [31].

$$D_{{CO_{2} {-}N_{2} }} = 0.235 \times 10^{ - 4} \;{\text{m}}^{2} /{\text{s}}$$
(25)
$$D_{{H_{2} S{-}N_{2} }} = 0.458 \times 10^{ - 4} \;{\text{m}}^{2} /{\text{s}}$$
(26)

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Bahlake, A., Farivar, F. & Dabir, B. New 3-dimensional CFD modeling of CO2 and H2S simultaneous stripping from water within PVDF hollow fiber membrane contactor. Heat Mass Transfer 52, 1295–1304 (2016). https://doi.org/10.1007/s00231-015-1635-y

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  • DOI: https://doi.org/10.1007/s00231-015-1635-y

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